JP4764128B2 - Fluid mixing device - Google Patents

Description

  The present invention relates to a fluid mixing device that distributes a fuel gas whose physical property value changes with time and mixes the fuel gas with a time delay.

  For example, in a general gas turbine combined cycle power generation facility, a gas turbine has a compressor, a combustor, and a turbine. Air that has become high pressure in the compressor, high pressure in the compressor, and heat Fuel gas heated to high temperature by the heater of the exchanger is sent to the combustor and combusted to drive the turbine. The high-temperature exhaust gas generated in the gas turbine is sent to the exhaust heat recovery boiler to generate steam, and the generated steam is sent to the steam turbine to operate the generator. Then, the condensate cooled by the steam turbine is returned to the exhaust heat recovery boiler and overheated, and steam is generated again and sent to the steam turbine.

  In such a power generation facility, it is considered to use a gas generated from an iron manufacturing plant as a fuel gas for a gas turbine. In this case, when the steel plant is a by-product gas generated in a direct reduction furnace (FINEX or COREX), the gas is low in calories and has a characteristic that the physical property value changes with time. A technique for stably burning the turbine is required.

JP 2000-140595 A

  As described above, when the gas generated from the steel manufacturing plant is used as the fuel gas of the gas turbine, it may be difficult to stably burn the gas turbine. That is, in a gas turbine, in order to realize required operation characteristics such as a generator output, fuel gas corresponding to high-pressure air is sent to a combustor and burned to drive the turbine. However, the by-product gas generated in the direct reduction furnace has a low calorie, and this calorie may change abruptly in time. In this case, the amount of heat input to the gas turbine changes abruptly. Therefore, the gas turbine cannot be stably burned. For this reason, it is necessary to supply this by-product gas to the gas turbine in a state in which the change in physical property value over time is relaxed.

  In addition, there exists the flow mixer described in the above-mentioned patent document 1 as what mixes different fluid uniformly, but this flow mixer adjusts the flow velocity of the fluid to mix arbitrarily, and mixes fluid uniformly. However, it does not equalize sudden changes in time in one kind of gas.

  The present invention solves the above-described problems, and an object of the present invention is to provide a fluid mixing apparatus that can be widely used by reducing the amount of change in fluid whose physical property value changes with time.

In order to achieve the above object, the fluid mixing apparatus according to the first aspect of the present invention includes an upstream pipe, a downstream pipe, a plurality of branch passages connecting the upstream pipe and the downstream pipe, and the upstream Fluid supply means for supplying and mixing the fluid introduced from the side pipe into the plurality of branch passages to the downstream side pipe at different times for each branch passage, and the fluid supply means includes the plurality of fluid pipes having different lengths. The plurality of branch passages have the same cross-sectional area, and the end portions are symmetrically connected to the outer peripheral surfaces of the upstream side pipe and the downstream side pipe at equal intervals in the circumferential direction. It is a feature.

In the fluid mixing apparatus according to a second aspect of the present invention, the fluid supply means is constituted by the plurality of branch passages having different volumes.

In the fluid mixing apparatus of the invention of claim 3, the fluid is a gas whose physical property value changes with time.

According to the fluid mixing device of the first aspect of the present invention, a plurality of branch passages for connecting the upstream side pipe and the downstream side pipe are provided, and the fluid introduced from the upstream side pipe to the plurality of branch passages is supplied to each branch passage. Provided with fluid supply means for supplying and mixing to the downstream pipe at different times , the fluid supply means is constituted by a plurality of branch passages having different lengths, and the plurality of branch passages have the same cross-sectional area and end portions Since the upstream pipe and the downstream pipe are connected symmetrically at equal intervals in the circumferential direction , the fluid introduced from the upstream pipe into the plurality of branch passages has different times for each branch passage by the fluid supply means. The downstream pipe is supplied and mixed. In the downstream pipe, the change amount of the fluid whose physical property value changes with time is relaxed, and this fluid can be widely used. In addition, the fluid introduced into the plurality of branch passages from the upstream side pipe is supplied to and mixed with the downstream side pipes at different times by the branch passages having different lengths. The amount of change in the fluid that changes can be reduced. Further, the fluid in the upstream side pipe is uniformly introduced into each of the symmetrically connected branch passages, and the change amount of the fluid whose physical property value changes with time can be moderated appropriately.

According to the fluid mixing device of the second aspect of the present invention, since the fluid supply means is constituted by a plurality of different branch passages, the fluid introduced into the plurality of branch passages from the upstream pipe has different times depending on the branch passages having different volumes. Therefore, the amount of change in the fluid whose physical property value changes with time can be reduced in the downstream side piping.

According to the fluid mixing device of the third aspect of the present invention, since the fluid is a gas whose physical property value changes over time, the amount of change in the physical property value of the gas whose physical property value changes over time can be moderated appropriately. .

  Exemplary embodiments of a fluid mixing apparatus according to the present invention will be described below in detail with reference to the accompanying drawings. Note that the present invention is not limited to the embodiments.

  1 is a schematic configuration diagram illustrating a fluid mixing apparatus according to a first embodiment of the present invention, FIG. 2 is a front view of the fluid mixing apparatus according to the first embodiment, and FIG. 3 is a graph illustrating a gas mixing ratio at a predetermined time. FIG. 4 is a graph showing a temporal change in the amount of heat in the byproduct gas and a temporal change in the amount of heat in the byproduct gas mixed by the fluid mixing apparatus of Example 1.

  The fluid mixing apparatus of Example 1 uses this by-product gas discharged from an iron manufacturing plant such as a direct reduction furnace (FINEX or COREX) as a gas turbine fuel gas in a gas turbine combined cycle power generation facility. The change in the physical property value of the by-product gas, whose physical property value changes with time, is relaxed and supplied to the gas turbine. This gas turbine combined cycle power generation facility is a plant that combines a gas turbine, an exhaust gas boiler, a steam turbine, and the like. That is, the amount of change in the by-product gas discharged from the steelmaking plant is reduced by the fluid mixing device of the first embodiment, and the change is sent to the combustor for combustion to drive the turbine. Then, the high-temperature exhaust gas generated in the gas turbine is sent to the exhaust heat recovery boiler to generate steam, and the generated steam is sent to the steam turbine to operate the generator. Then, the condensate cooled by the steam turbine is returned to the exhaust heat recovery boiler and overheated, and steam is generated again and sent to the steam turbine.

  In the fluid mixing apparatus of the first embodiment applied to such a gas turbine combined cycle power generation facility, as shown in FIGS. 1 and 2, the upstream pipe 11 has an upstream end connected to a steel plant not shown. On the other hand, the downstream end is closed, and a by-product gas (fluid) generated in the steel plant flows. The downstream end of the downstream pipe 12 is closed, while the downstream end is connected to a combustor of a gas turbine (not shown). In this case, the by-product gas generated in the steel plant is a gas whose physical property value changes with time.

  The downstream end of the upstream pipe 11 and the upstream end of the downstream pipe 12 are connected by a plurality of (10 in this embodiment) branch passages 21 to 30. Each of the branch passages 21 to 30 has one end connected to the outer peripheral surface of the upstream pipe 11 and the other end connected to the outer peripheral surface of the downstream pipe 12. Each end of 30 is connected symmetrically with respect to the upstream pipe 11 and the downstream pipe 12. That is, the ends of the branch passages 21 to 30 are connected to the outer peripheral surfaces of the upstream pipe 11 and the downstream pipe 12 at equal intervals in the circumferential direction.

  Further, the branch passages 21 to 30 supply and mix the fluid introduced from the upstream pipe 11 to the branch passages 21 to 30 to the downstream pipe 12 at different times for each branch passage 21 to 30. It has fluid supply means. In this embodiment, the fluid supply means is constituted by the branch passages 21 to 30 having different lengths.

That is, the axial length L of each of the branch passages 21 to 30 is the same, but the radial lengths R _{1 to} R ₁₀ are different and have the following relationship. In addition, the internal diameter of each branch channel | path 21-30, ie, cross-sectional area, is the same, and is uniform also in the longitudinal direction.
R ₁₀ = 10R ₁
R ₉ = 9R ₁
R ₈ = 8R ₁
R ₇ = 7R ₁
R ₆ = 6R ₁
R ₅ = 5R ₁
R ₄ = 4R ₁
R ₃ = 3R ₁
R ₂ = 2R ₁

  Therefore, the by-product gas flowing through the upstream pipe 11 is branched at the downstream end thereof, introduced into the branch passages 21 to 30, and supplied to the downstream pipe 12 through the branch passages 21 to 30 to join. To do. At this time, since the lengths of the branch passages 21 to 30 are different, the by-product gas introduced from the upstream pipe 11 to the branch passages 21 to 30 reaches the downstream pipe 12 with a time delay. That is, as shown in FIG. 3, the by-product gas supplied to the downstream pipe 12 through the branch passages 21 to 30 is shifted by the delay time S and reaches the downstream pipe 12. In FIG. 12, different gases in time are mixed, and the amount of change in the physical property value of the by-product gas is alleviated, and the heat amount is averaged over time. That is, the by-product gas in the upstream pipe 11 is supplied to the downstream pipe 12 with a time delay through the branch passages 21 to 30, so that the by-product gas in the upstream pipe 11 is subjected to a moving average process in a predetermined period. This means that the downstream pipe 12 joins.

  In this case, the length in each of the branch passages 21 to 30 may be determined by the flow rate of the byproduct gas and the necessary shift time (delay time) S. Further, the number of the branch passages 21 to 30 is obtained as T / S + 1 by the time T for performing the moving average process and the shift time S.

  Here, the operation of the fluid mixing apparatus of the present embodiment will be specifically described. As shown in FIG. 4, the amount of heat of the by-product gas (measured value) before performing the processing by the fluid mixing apparatus of the present embodiment changes rapidly with time. On the other hand, the by-product gas (moving average value) after the treatment by the fluid mixing apparatus of the present embodiment is moderated in the amount of heat, suppressed in time, and has a small change width. In this case, when the amount of heat at times t1, t2, t3, t4, and t5 is y1, y2, y3, y4, and y5, the moving average value Y in the period from t1 to t5 is (y1 + y2 + y3 + y4 + y5) / 5. .

  As described above, in the fluid mixing device according to the first embodiment, the downstream end portion of the upstream side pipe 11 connected to the steel plant and the upstream end portion of the downstream side pipe 12 connected to the gas turbine include a plurality of By connecting the branch passages 21 to 30 and changing the lengths of the branch passages 21 to 30, the fluid introduced from the upstream side pipe 11 to the branch passages 21 to 30 is supplied to the branch passages 21 to 30. Each is supplied to the downstream pipe 12 with a different delay time and mixed.

  Therefore, when the by-product gas flowing through the upstream pipe 11 is branched at the downstream end thereof, introduced into the branch passages 21 to 30, and supplied to the downstream pipe 12 through the branch passages 21 to 30. Since the lengths of the branch passages 21 to 30 are different, the by-product gas is supplied to the downstream pipe 12 with a time delay, and the physical property value of the by-product gas, that is, the amount of heat is subjected to a moving average process. As a result, the amount of change is relaxed, and the amount of heat averaged over time can be obtained.

  In the present embodiment, the length of the branch passages 21 to 30 is made different so that the by-product gas is supplied to the downstream side pipe 12 with a time delay, and the by-product gas has a simple configuration. The amount of heat can be reduced by moving average processing.

  In the present embodiment, one end of each branch passage 21 to 30 is connected to the outer peripheral surface of the upstream pipe 11, while the other end is connected to the outer peripheral surface of the downstream pipe 12, and each branch passage 21 to 30 is connected. Are connected so as to be symmetrical with respect to the upstream pipe 11 and the downstream pipe 12. Therefore, the by-product gas flowing through the upstream pipe 11 can be uniformly distributed and introduced into the branch passages 21 to 30, and the by-product gas can be subjected to a moving average process with high accuracy.

  In the above-described first embodiment, ten branch passages 21 to 30 having a U-shape are provided. However, the shape and the number of the branch passages 21 to 30 are not limited thereto. This branch passage only needs to be able to supply and mix the fluid from the upstream side pipe to the downstream side pipe at different times for each branch passage having a different length. For example, the branch passage may have a curved shape or a spiral shape.

  5 is a schematic configuration diagram illustrating a fluid mixing apparatus according to Embodiment 2 of the present invention, FIG. 6 is a cross-sectional view taken along the line VI-VI in FIG. 5, and FIG. 7 is a cross-sectional view taken along the line VII-VII in FIG.

  In the fluid mixing apparatus of the second embodiment, as shown in FIGS. 5 to 7, the upstream pipe 41 connected to an iron manufacturing plant (not shown) is closed at the downstream end thereof, and the by-product generated in the iron manufacturing plant. Gas (fluid) flows. An upstream end of the downstream pipe 42 connected to the combustion gas of a gas turbine (not shown) is closed. In this case, the by-product gas generated in the steel plant is a gas whose physical property value changes with time.

  A tank 43 is disposed between the upstream side pipe 41 and the downstream side pipe 42, and the downstream end portion of the upstream side pipe 41 and the upper portion of the tank 43 have a plurality of (in this embodiment, ten) The first branch passages 51 to 60 are connected, and the lower portion of the tank 43 and the upstream end portion of the downstream pipe 42 are connected by a plurality of (in this embodiment, ten) second branch passages 61 to 70. Each of the first branch passages 51 to 60 has one end connected to the outer peripheral surface of the upstream pipe 41, and the other end connected to the center of the upper surface of the tank 43. 70 equally connects the upstream piping 41 and the tank 43, and the tank 43 and the downstream piping 42, respectively. That is, each branch passage 51 to 60 has the same length, pipe diameter, and number of bends (bends), and the same applies to each branch passage 61 to 70.

  Further, the tank 43 supplies the fluid introduced from the upstream side pipe 41 through the first branch passages 51 to 60 to the downstream side pipe 42 through the second branch passages 61 to 70 at different times. And fluid supply means for mixing. In this embodiment, the fluid supply means is constituted by the tanks 43 partitioned so as to have different volumes from the respective branch passages 51 to 60 and 61 to 70.

That is, the tank 43 is divided into 10 chambers 71 to 80 by 10 partition walls 43a to 43j with the center portion as a fulcrum, and the end portions of the first branch passages 51 to 60 are on the center side of the chambers 71 to 80. On the other hand, the ends of the second branch passages 61 to 70 are connected to the outer peripheral side of the rooms 71 to 80. Then, they have different volume Q ₁ ~Q ₁₀ of each room 71 to 80, and has a relationship of the following.
Q ₁₀ = 10Q ₁
Q ₉ = 9Q ₁
Q ₈ = 8Q ₁
Q ₇ = 7Q ₁
Q ₆ = 6Q ₁
Q ₅ = 5Q ₁
Q ₄ = 4Q ₁
Q ₃ = 3Q ₁
Q ₂ = 2Q ₁

  Therefore, the by-product gas flowing through the upstream pipe 41 is branched at the downstream end portion thereof and introduced into the chambers 71 to 80 of the tank 43 via the first branch passages 51 to 60, and the chambers 71 to 80. It moves to the outside and is supplied to the downstream pipe 42 via the second branch passages 61 to 70 and merges. At this time, since the volumes of the rooms 71 to 80 are different, the by-product gas introduced from the upstream pipe 11 into the rooms 71 to 80 of the tank 43 via the first branch passages 51 to 60 is temporal. The downstream pipe 12 is reached via the second branch passages 61 to 70 with a delay.

  That is, as in the first embodiment, the by-product gas supplied to the downstream pipe 42 through the chambers 71 to 80 of the tank 43 is shifted by a predetermined delay time and reaches the downstream pipe 42. In this downstream pipe 42, different gases in time are mixed, and the amount of change in the physical property value of the by-product gas is alleviated, and the heat amount is averaged over time. That is, the by-product gas in the upstream pipe 41 is supplied to the downstream pipe 42 with a time delay by the rooms 71 to 80, so that the by-product gas in the upstream pipe 41 is subjected to a moving average process in a predetermined period. That is, the downstream pipe 42 joins.

  As described above, in the fluid mixing apparatus according to the second embodiment, a plurality of chambers 71 to 80 are defined between the upstream pipe 41 connected to the steel plant and the downstream pipe 42 connected to the gas turbine. The tank 43 is provided, the downstream end of the upstream pipe 41 and the upper part of each room 71-80 of the tank 43 are connected by the first branch passages 51-60, and the lower part of each room 71-80 of the tank 43 is connected downstream. The upstream end of the side pipe 42 is connected to each of the second branch passages 61 to 70, and the volumes of the chambers 71 to 80 of the tank 43 are made different. The fluid introduced to -80 is supplied to the downstream pipe 42 with different delay time for each of the rooms 71-80, and mixed.

  Accordingly, the by-product gas flowing through the upstream pipe 41 is branched at the downstream end thereof, introduced into the respective rooms 71 to 80 of the tank 43, and supplied to the downstream pipe 42 through the respective rooms 71 to 80. Since the volumes of the rooms 71 to 80 are different, the by-product gas is supplied to the downstream pipe 42 with a time delay, and the physical property value of the by-product gas, that is, the amount of heat is subjected to a moving average process. As a result, the amount of change is relaxed, and the amount of heat averaged over time can be obtained.

  In the present embodiment, the volumes of the chambers 71 to 80 of the tank 43 are made different so that the by-product gas is supplied to the downstream pipe 42 with a time lag, and the sub-structure gas is simply configured. It is possible to reduce the amount of change by moving and averaging the amount of heat of the raw gas, and to suppress an increase in the size of the apparatus.

  In the above-described second embodiment, each of the rooms 71 to 80 of the tank 43 is divided into ten, but the number is not limited thereto. Moreover, by-product gas flow paths are formed in the chambers 71 to 80 of the tank 43 by partition plates, so that the by-product gas introduced into the chambers 71 to 80 can be reliably discharged with a time delay. it can.

  FIG. 8 is a schematic configuration diagram illustrating a fluid mixing apparatus according to Embodiment 3 of the present invention. In addition, the same code | symbol is attached | subjected to the member which has the same function as what was demonstrated in Example 2 mentioned above, and the overlapping description is abbreviate | omitted.

  In the fluid mixing apparatus of the third embodiment, as shown in FIG. 8, a tank 43 is disposed below the upstream pipe 41 and the downstream pipe 42, and the downstream end of the upstream pipe 41 and the tank 43 The central portion of the upper surface is connected by the first branch passages 51 to 60, and the downstream pipe 42 and the outer peripheral portion of the upper surface of the tank 43 are connected by the second branch passages 61 to 70. In this case, the inside of the tank 43 is partitioned into the rooms 71 to 80, and the end portions of the first branch passages 51 to 60 are connected to the center side of the rooms 71 to 80, while the second branch passages 61 to 70 are connected. Is connected to the outer peripheral side of the rooms 71-80.

  Therefore, the by-product gas flowing through the upstream pipe 41 is branched at the downstream end portion thereof and introduced into the chambers 71 to 80 of the tank 43 via the first branch passages 51 to 60, and the chambers 71 to 80. It moves to the outside and is supplied to the downstream pipe 42 via the second branch passages 61 to 70 and merges. At this time, since the volumes of the rooms 71 to 80 are different, the by-product gas introduced from the upstream pipe 11 into the rooms 71 to 80 of the tank 43 via the first branch passages 51 to 60 is temporal. The downstream pipe 12 is reached via the second branch passages 61 to 70 with a delay.

  That is, the by-product gas supplied to the downstream side pipe 42 through the chambers 71 to 80 of the tank 43 is shifted by a predetermined delay time and reaches the downstream side pipe 42. Different gases are mixed with each other, and the amount of change in the physical property value of the by-product gas is alleviated, and the heat amount is almost averaged. That is, the by-product gas in the upstream pipe 41 is supplied to the downstream pipe 42 with a time delay by the rooms 71 to 80, so that the by-product gas in the upstream pipe 41 is subjected to a moving average process in a predetermined period. Then, the downstream pipe 42 joins.

  As described above, in the fluid mixing apparatus according to the third embodiment, the downstream end of the upstream pipe 41 and the center of the upper surface of each chamber 71 to 80 of the tank 43 are connected by the first branch passages 51 to 60, By connecting the upstream end portion of the side pipe 42 and the outer peripheral portion of the upper surface of each chamber 71 to 80 of the tank 43 by the second branch passages 61 to 70, the volumes of the chambers 71 to 80 of the tank 43 are made different. The fluid introduced from the upstream side pipe 41 to the respective chambers 71 to 80 of the tank 43 is supplied to the downstream side pipe 42 and mixed with different delay times for each of the rooms 71 to 80.

  Accordingly, the by-product gas flowing through the upstream pipe 41 is branched at the downstream end thereof, introduced into the respective rooms 71 to 80 of the tank 43, and supplied to the downstream pipe 42 through the respective rooms 71 to 80. Since the volumes of the rooms 71 to 80 are different, the by-product gas is supplied to the downstream pipe 42 with a time delay, and the physical property value of the by-product gas, that is, the amount of heat is subjected to a moving average process. As a result, the amount of change is relaxed, and the amount of heat averaged over time can be obtained.

  Further, the ends of the upstream pipe 41 and the downstream pipe 42 are connected to the upper surfaces of the tank 43 corresponding to the chambers 71 to 80, and the degree of freedom in layout of the upstream pipe 41, the downstream pipe 42, and the tank 43. Can be improved.

  In each of the above-described embodiments, a plurality of fluid pipes having different lengths are used as fluid supply means for supplying and mixing the fluid introduced from the upstream pipe into the plurality of branch passages to the downstream pipe at different times for each branch passage. Although the branch passages 21 to 30 or the rooms 71 to 80 of the tank 43 having different volumes are applied, the present invention is not limited to this configuration. For example, a plurality of branch passages having different channel cross sections, a plurality of branch passages having different channel resistances, and the like may be used.

  The fluid mixing device according to the present invention distributes fluids and mixes them at different times, and can be applied as a fluid mixing device that mixes various fluids.

It is a schematic block diagram showing the fluid mixing apparatus which concerns on Example 1 of this invention. 1 is a front view of a fluid mixing apparatus of Example 1. FIG. It is a graph showing the gas mixture ratio in predetermined time. It is a graph showing the time change of the calorie | heat amount in byproduct gas, and the time change of the calorie | heat amount in the byproduct gas mixed by the fluid mixing apparatus of Example 1. It is a schematic block diagram showing the fluid mixing apparatus which concerns on Example 2 of this invention. It is VI-VI sectional drawing of FIG. It is VII-VII sectional drawing of FIG. It is a schematic block diagram showing the fluid mixing apparatus which concerns on Example 3 of this invention.

Explanation of symbols

11, 41 Upstream piping 12, 42 Downstream piping 21-30 Branch passage (fluid supply means)
43 Tanks 51-60 First branch passage (fluid supply means)
61-70 Second branch passage (fluid supply means)
71-80 rooms (fluid supply means)

Claims (3)

An upstream pipe, a downstream pipe, a plurality of branch passages connecting the upstream pipe and the downstream pipe, and a fluid introduced from the upstream pipe into the plurality of branch passages for each branch passage Fluid supply means for supplying and mixing to the downstream pipe at different times ,
The fluid supply means is constituted by the plurality of branch passages having different lengths,
The plurality of branch passages have the same cross-sectional area, and end portions are symmetrically connected to the outer peripheral surfaces of the upstream pipe and the downstream pipe at equal intervals in the circumferential direction .   2. The fluid mixing apparatus according to claim 1, wherein the fluid supply means is constituted by the plurality of branch passages having different volumes. 3. The fluid mixing apparatus according to claim 1 , wherein the fluid is a gas whose physical property value changes with time.

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